TW201736770A - Method of controlling pressure within a pressure vessel - Google Patents

Abstract

A method of controlling pressure within a pressure vessel includes introducing a flushing fluid stream into a pressure vessel, wherein the pressure vessel comprises a vapor injection valve and a vapor release valve; passing a first vapor stream through the vapor injection valve and into the pressure vessel when a pressure within the pressure vessel reaches a minimum value; passing a second vapor stream through the vapor release valve and out of the pressure vessel when the pressure within the pressure vessel reaches a maximum value, wherein the minimum value and the maximum value are different.

Description

Method of controlling pressure in a pressure vessel

This case relates to a method of controlling the pressure in a pressure vessel.

Pressure vessels are used in a variety of industrial and private sector applications. Pressure vessels appear in these sectors as industrial compressed air receivers and domestic hot water storage tanks. Examples of other pressure vessels are submersibles, recompression chambers, distillation columns, pressure reactors, autoclaves, and many other vessels in mining operations, refineries and petrochemical plants, nuclear reactor vessels, submarines and spacecraft cabins. , air pressure storage, hydraulic tank under pressure, rail car air brake storage, road vehicle air brake storage, and storage containers for liquefied gases (such as ammonia, chlorine, and liquid petroleum gas).

Conventional pressure control methods often involve non-variable or static pressure control systems. These methods increase or release pressure from the container whenever a certain internal pressure value is reached. This pressure value is a single static value. These static systems result in significant lack of efficiency and economic loss. For example, the pressure in the container must be adjusted very frequently. This results in overuse of the pressure regulating flow and also allows a significant amount of stored material to escape from the container.

In particular in connection with the manufacture of oligomers and/or polymers (for example, polymerization of ethylene, or oligomerization of ethylene, for example, selective ethylene di-, tri- and tetra-polymerization for the production of comonomer-grade linear alpha-olefins) In technology, equipment fouling is a problem and is often encountered. In such processes, waxes and polymers are inherent by-products that cannot be completely avoided. These waxes and polymers can cause fouling of the reactor itself as well as surrounding and downstream equipment. In the worst case, some of the equipment, such as the pipe, is blocked in the subsequent process section, with the consequence that the process must be shut down.

In the polymerization of ethylene and/or other alpha-olefins, the deposition of polymer solids can also occur in reactors and/or equipment having various pressure variations.

In order to control the deposit of polymer and wax, the reactor must be cleaned regularly. In order to avoid any long downtime, an alternate reactor is required to prevent any manufacturing losses.

With regard to cleaning reactors with solid deposits (e.g., high molecular weight oligomers/polymers), the reactor must be opened to date, and typically the plant personnel must enter the reactor for mechanical cleaning. After cleaning, the reactor must be rendered inert again. The reason is that any traces of moisture and oxygen will poison the highly sensitive organometallic catalyst used for oligomerization and polymerization. This program is very time consuming. In summary, typical reactor downtimes are about one week or longer, resulting in considerable total productivity loss.

To overcome these disadvantages, procedures for avoiding any mechanical cleaning include introducing a hot solvent having a temperature of at least about 75 ° C into the reactor to dissolve the polymer deposits. After cleaning, the solvent can be, for example, steamed Distillation, crystallization, thin film evaporation, wiped-film evaporation, and/or falling film evaporation are recovered in a solvent recovery unit.

This method works in a satisfactory manner as long as the polymer solid material has a sufficiently short carbon chain length. This is especially true for zirconium-based catalyst systems, which typically only provide relatively short chain lengths of polyethylene and wax. However, this can be changed if trace levels of impurities are introduced intrinsically (via raw material impurities) or unintentionally (caused by destabilizing process conditions) into the oligomerization reactor. In particular, traces of moisture, air and/or corrosion products can induce the formation of relatively long-chain and potentially branched polyethylenes that are relatively poorly soluble in aromatic solvents.

The use of other catalyst systems, such as chromium-based catalyst systems, for selective three or four polymerization of ethylene can greatly exacerbate this situation. Although only a small amount of polyethylene is formed in compliance with specifications, Cr-induced polymers tend to have longer chain lengths and greatly slow the morphological characteristics of the dissolution process.

Conventional pressure control methods in irrigation systems involve non-variable or static pressure control systems. These methods increase or release pressure from the container whenever a certain internal pressure value is reached. These static systems result in significant lack of efficiency and economic loss. For example, the pressure in the container must be adjusted very frequently. This results in overuse of the pressure regulating flow and also allows a significant amount of stored material to escape from the container.

Accordingly, there is a need for a method of effectively controlling the pressure in a pressure vessel that significantly reduces the use of pressure regulating flow and the amount of stored material lost due to frequent pressure adjustments.

Methods of controlling the pressure in a pressure vessel and methods of flushing the reactor are disclosed in various specific aspects.

A method of controlling pressure in a pressure vessel, comprising: introducing a flow of a flushing fluid into a pressure vessel, wherein the pressure vessel comprises a vapor injection valve and a vapor release valve; and when the pressure in the pressure vessel reaches a minimum, passing the first vapor stream The vapor is injected into the valve and into the pressure vessel; when the pressure in the pressure vessel reaches a maximum, the second vapor stream is passed through the vapor release valve and exits the pressure vessel, wherein the minimum value and the maximum value are different of.

A method of rinsing a reactor, comprising: introducing a flow of a flushing fluid into a pressure vessel, wherein the pressure vessel comprises a vapor injection valve and a vapor release valve; and when the pressure in the pressure vessel reaches a minimum, the first vapor stream is injected through the vapor The valve enters the pressure vessel; when the pressure in the pressure vessel reaches a maximum, the second vapor stream is passed through the vapor release valve and exits the pressure vessel, wherein the minimum value and the maximum value are different; The pressure vessel draws a portion of the flushing fluid stream; and the portion of the flushing fluid stream is passed through the reactor to flush the reactor.

These and other features and features are described in more detail below.

10‧‧‧ Pressure control method

12‧‧‧ fluid flushing flow

14‧‧‧ Pressure vessel

16‧‧‧First vapor stream

18‧‧‧Vapor injection valve

20‧‧‧Second vapor flow

22‧‧‧Vapor release valve

24‧‧‧ merged line

26‧‧‧ pump

28‧‧‧heater

30‧‧‧Flow controller

32‧‧‧Reactor

The following is a brief description of the drawings in which like elements are numbered similarly and are presented for the purpose of illustrating the exemplary embodiments disclosed herein. The purpose of the body, not the purpose of limiting it.

1 is a simplified schematic diagram showing a pressure control method in accordance with the present disclosure.

The methods disclosed herein provide a means of effectively controlling the pressure in a pressure vessel that reduces the use of pressure regulating flow and the amount of stored material that is lost due to frequent pressure adjustments. For example, the methods disclosed herein can include a variable pressure control system. For example, the method can include using a variable pressure between the two sets of minimum and maximum points. This can be advantageous compared to static pressure because the use of static pressure typically results in the use of more nitrogen, and more toluene is lost when the pressure valve is opened and closed to balance the static pressure. With the method of the present invention, different control types than static control can be used to reduce the amount of stored material lost due to pressure adjustment. This method reduces the frequency of pressure adjustments required. The disclosed method reduces the amount of material injected into the pressure vessel for pressure adjustment purposes. For example, the methods disclosed herein can reduce the amount of nitrogen consumed by greater than or equal to 90%. This method also reduces the amount of stored material lost from the container during frequent pressure adjustments. For example, the methods disclosed herein can reduce the amount of toluene lost from the pressure vessel by greater than or equal to 45%.

The pressure control method disclosed herein can include introducing a flow of irrigation fluid into a pressure vessel. The pressure vessel can include a vapor injection valve and a vapor release valve. The first vapor stream can then be passed through the vapor injection valve and into the pressure vessel when the pressure in the pressure vessel reaches a minimum. when When the pressure in the pressure vessel reaches a maximum, a second vapor stream can be released through the vapor release valve and exit the pressure vessel. The minimum and the maximum may be the same or different. A portion of the flushing fluid stream can be withdrawn from the pressure vessel and flushed through the reactor.

The pressure control methods disclosed herein can include fluid flow. For example, the fluid stream can comprise a solvent, such as an aromatic solvent. For example, the fluid stream can comprise toluene as a solvent in the oligomerization reaction. The fluid stream can comprise a flushing fluid. For example, the fluid stream can comprise toluene for flushing the reactor and heat exchanger. The flushing fluid stream can comprise any aromatic solvent. The fluid stream can comprise any organic liquid having a boiling point of less than or equal to 300 ° C at atmospheric pressure. For example, the fluid stream can comprise an aromatic solvent, an organic liquid having a boiling point of less than or equal to 300 ° C, or a combination comprising at least one of the foregoing.

The pressure control method described herein can include a pressure vessel. For example, a fluid stream can be passed through the pressure vessel. For example, the pressure vessel can be a toluene storage vessel. The pressure vessel can comprise steel, a composite material, a polymeric material, or a combination comprising at least one of the foregoing. The temperature in the container can be greater than or equal to 50 °C. For example, the temperature in the container can be greater than or equal to 80 °C. For example, the temperature in the container can range from 80 °C to 250 °C. The pressure vessel can contain a valve. For example, the pressure vessel can contain more than or equal to one valve. For example, the pressure vessel can contain 2 valves. The valve can be an injection valve, a release valve, or a combination comprising at least one of the foregoing. For example, the pressure vessel can include an injection valve and a flare depressurization valve.

The pressure control method disclosed herein can include passing a stream through a valve and into a pressure vessel. For example, a vapor stream can be passed through a vapor injection valve and into a pressure vessel. The vapor stream can comprise an inert gas. For example, the vapor stream can comprise nitrogen, methane gas, ethane gas, or a combination comprising at least one of the foregoing. When the pressure in the pressure vessel reaches a minimum, the vapor stream can be passed through an injection valve and into the pressure vessel. The injection of this vapor stream increases the pressure in the pressure vessel.

The pressure control method disclosed herein can include passing a stream through a valve to release the stream from a pressure vessel. For example, the vapor stream can be passed through a flared pressure relief valve to release the vapor stream from the pressure vessel. The vapor stream released from the pressure vessel may comprise a fluid in the gas phase that is stored in the pressure vessel, an inert gas, or a combination comprising at least one of the foregoing. For example, the vapor stream released from the pressure vessel can comprise nitrogen and gaseous toluene. When the pressure in the pressure vessel reaches a maximum, the vapor stream can be released from the pressure vessel through a flared pressure relief valve. The release of this vapor stream reduces the pressure in the pressure vessel.

The pressure control methods disclosed herein can include variable, non-static pressure control systems. For example, the minimum pressure value and the maximum pressure value in the pressure vessel can be different values. For example, the minimum pressure value can range from 10 kPa to 500 kPa. For example, the minimum pressure value can range from 300 kPa to 400 kPa. For example, the minimum pressure value can be 350 kPa. The maximum pressure can range from 50 kPa to 1000 kPa. For example, the maximum pressure value can range from 600 kPa to 700 kPa. For example, the maximum pressure value can be 650 kPa. The minimum pressure value and the maximum pressure value may differ by, for example, greater than or equal to 10 kPa. For example, the values can differ by more than or equal to 300 kPa.

The pressure control method disclosed herein can include withdrawing a fluid stream from a pressure vessel. For example, the methods disclosed herein can include withdrawing a stream of flushing fluid comprising toluene from a pressure vessel. The fluid stream can pass more than or equal to one pump. For example, the fluid stream can be propelled by more than or equal to one pump. For example, the fluid stream can be propelled by 2 pumps. The pump can be operated independently of the pressure in the pressure vessel. For example, changes in pump suction pressure will not affect the flow of fluid from the pressure vessel (changes in pressure in the pressure vessel also have no effect on pump performance). This fluid stream can pass through a heat exchanger. For example, the fluid stream can be passed through a heater to increase the temperature of the fluid stream.

The pressure control methods disclosed herein can include the purpose of passing a fluid stream through a reactor or heat exchanger for rinsing. This fluid stream can be used as a solvent stream. For example, the fluid stream can be used as a solvent stream for the oligomerization reactor. The fluid stream can be returned to the pressure vessel as part of a closed loop system after passing through the reactor or heat exchanger. The flow of fluid flow can be controlled by a flow controller.

The process can be used to clean reactors and/or equipment for oligomerization or polymerization. The oligomeric polymerization should comprise an olefin, such as ethylene, which is polymerized in two, three and four to produce a linear alpha olefin. Polymerization includes the polymerization of ethylene and other alpha-olefins as well as their copolymerization.

In oligomeric polymerization, polymer residues are inherently formed as by-products that can form deposits in the reactor and/or equipment. During the polymerization, the product itself (polymer) can form its own deposit. In both the oligomerization and polymerization processes, the reactor and/or equipment must be cleaned to Avoid blocking it.

A more complete understanding of the components, methods, and instrumentologies disclosed herein can be obtained by reference to the accompanying drawings. The drawings (also referred to herein as "figure") are merely schematic representations based on the convenience and ease of illustration of the present disclosure, and thus are not intended to indicate the relative size and size and/or definition or limitation of the components of the device. Illustrative range of specific aspects. The specific terminology used in the following description is for the purpose of illustration and description In the following figures and the following description, it should be understood that like reference numerals refer to the

Referring now to FIG. 1, the pressure control method 10 disclosed herein can include passing a fluid flushing stream 12 through a pressure vessel 14. For example, fluid flushing stream 12 can comprise toluene and pressure vessel 14 can be a toluene storage vessel. The method disclosed herein can include passing the first vapor stream 16 through a vapor injection valve 18. For example, the first vapor stream 16 can comprise nitrogen. The first vapor stream 16 can be passed through the vapor injection valve 18 and into the pressure vessel 14 via the merge line 24. For example, the first vapor stream 16 can be passed to the pressure vessel 14 when the pressure in the pressure vessel 14 reaches a minimum.

The pressure control method disclosed herein can include passing the second vapor stream 20 through the vapor release valve 22. For example, the second vapor stream 20 can comprise gaseous nitrogen and gaseous toluene. For example, the second vapor stream 20 can exit the pressure vessel 14 via the merge line 24 and then pass through the vapor release valve 22. For example, the second vapor stream 20 can exit the pressure vessel 14 when the pressure in the pressure vessel 14 reaches a maximum. For example, the maximum pressure value and the minimum pressure Values can be different values.

The pressure control method disclosed herein can include withdrawing the fluid flushing stream 12 from the pressure vessel 14. Fluid flushing stream 12 can then be passed through pump 26. For example, fluid flushing stream 12 can be propelled by pump 26. Pump 26 can operate independently of the pressure in pressure vessel 14. Fluid flushing stream 12 can also be passed through heater 28. The pressure control method 10 can be a closed loop system.

The pressure control method disclosed herein can include passing a fluid flushing stream 12 through reactor 32 to flush reactor 32. The flow of fluid flushing stream 12 to reactor 32 can be controlled by flow controller 30. The fluid flushing stream 12 can be passed through the reactor 32 and then fed back to the pressure vessel 14 as part of the closed loop pressure control method 10.

The following examples are merely illustrative of the pressure control methods disclosed herein and are not intended to limit the scope thereof.

Example Comparative Example 1

Pressure control methods in conventional pressure vessels are used for the purposes of this comparative example. A static, non-variable pressure control system is used. The toluene storage pressure vessel was operated at a fixed pressure of 510 kPa. Nitrogen is injected into the container to increase the pressure in the container, while the release valve is opened to reduce the pressure. Two separate tests, Test 1 and Test 2, were performed using this method. The test was conducted one month apart. The results of the two tests are described in Table 1. The total amount of nitrogen consumed is expressed in kilograms per day. The total ventilation flow is expressed in kilograms per day. The toluene concentration is expressed in mass percent. Toluene consumed The total amount is expressed in kilograms per day. The temperature was held constant at 155 °C.

Example 1

The pressure control method according to the present disclosure, as described in FIG. 1, is used for the purpose of the present embodiment. A variable, non-static pressure control system is used. Nitrogen injection is used to increase the pressure in the toluene vessel. Use a pressure relief valve to reduce pressure. The maximum pressure is set at 650 kPa and the minimum pressure is set at 350 kPa. The net positive suction height difference of the container is 20 meters, and the required net positive suction height difference is 5.3 meters. The temperature in the vessel was 155 °C. The results are described in Table 1 as Test 3. It can be seen that the method disclosed herein (Test 3) significantly reduces the amount of material that must be injected into the pressure vessel for pressure adjustment purposes (compared to Test 1 and Test 2). For example, the methods disclosed herein can reduce the amount of nitrogen consumed by greater than or equal to 90%. The methods disclosed herein can also significantly reduce the amount of stored material lost from the container during frequent pressure adjustments. For example, the methods disclosed herein can reduce the amount of toluene lost from the pressure vessel by greater than or equal to 45%.

The methods disclosed herein include at least the following specific aspects:

Aspect 1: A method of controlling pressure in a pressure vessel, comprising: introducing a flow of a flushing fluid into a pressure vessel, wherein the pressure vessel comprises a vapor injection valve and a vapor release valve; when the pressure in the pressure vessel reaches a minimum value Passing a first vapor stream through the vapor injection valve and into the pressure vessel; and when the pressure in the pressure vessel reaches a maximum, passing a second vapor stream through the vapor release valve and exiting the pressure vessel, wherein The minimum value and the maximum value are different.

2: The method of the specific aspect 1, wherein the rinsing fluid stream comprises an aromatic solvent, an organic liquid having a boiling point lower than or equal to 300 ° C, or a combination comprising at least one of the foregoing, preferably wherein the rinsing The fluid contains toluene.

The method of any one of the preceding aspects, wherein the first vapor stream comprises an inert gas, preferably wherein the first vapor stream comprises nitrogen, methane, ethane, or at least A combination of the foregoing.

The method of any one of the preceding claims, wherein the second vapor stream comprises the flushing fluid in a gas phase.

The method of any one of the preceding aspects, wherein the temperature in the pressure vessel is from 80 ° C to 250 ° C.

The method of any one of the preceding aspects, wherein the pressure in the pressure vessel has a minimum value of from 10 kPa to 500 kPa.

Concrete aspect 7: Any of the foregoing specific aspects The method wherein the pressure in the pressure vessel has a maximum value of from 50 kPa to 1000 kPa.

The method of any one of the preceding aspects, wherein the minimum value of the pressure in the pressure vessel differs from the maximum value of the pressure in the pressure vessel by greater than or equal to 10 kPa.

A method of any one of the preceding aspects, wherein the flushing fluid stream is propelled by a pump, wherein the pump operates independently of the pressure in the pressure vessel.

The method of any one of the preceding aspects, wherein the pressure vessel comprises steel, a composite material, a polymeric material, or a combination comprising at least one of the foregoing.

A specific aspect 11 is a method of rinsing a reactor, comprising: introducing a flow of a flushing fluid into a pressure vessel, wherein the pressure vessel comprises a vapor injection valve and a vapor release valve; when the pressure in the pressure vessel reaches a minimum value, a vapor stream passing through the vapor injection valve and into the pressure vessel; when the pressure in the pressure vessel reaches a maximum, passing a second vapor stream through the vapor release valve and exiting the pressure vessel, wherein the minimum value and the The maximum value is different; a portion of the flushing fluid stream is withdrawn from the pressure vessel; and the portion of the flushing fluid stream is passed through the reactor to flush the reactor.

Aspect 12: The method of Embodiment 11, wherein the extracted portion of the flushing fluid is monitored by a flow controller prior to passing through the reactor.

Specific Aspect 13: The method of Concrete Aspect 11 or Aspect 12, wherein the reactor is flushed as a closed loop system.

The method of any one of the aspects 11-13, wherein the rinsing fluid stream comprises an aromatic solvent, an organic liquid having a boiling point lower than or equal to 300 ° C, or a combination comprising at least one of the foregoing Preferably, the rinse fluid comprises toluene.

The method of any one of aspects 11-14, wherein the first vapor stream comprises an inert gas, preferably wherein the first vapor stream comprises nitrogen, methane, ethane, or A combination comprising at least one of the foregoing.

The method of any one of the aspects 11-15, wherein the temperature in the pressure vessel is from 80 ° C to 250 ° C.

The method of any one of the aspects 11-16, wherein the pressure in the pressure vessel has a minimum value of 10 kPa to 500 kPa.

The method of any one of the aspects 11-17, wherein the pressure in the pressure vessel has a maximum value of 50 kPa to 1000 kPa.

The method of any one of aspects 11-18, wherein the minimum value of the pressure in the pressure vessel differs from the maximum value of the pressure in the pressure vessel by greater than or equal to 10 kPa.

The method of any one of aspects 11-19, wherein the flushing fluid flow is advanced by a pump, wherein the pump operates independently of the pressure in the pressure vessel.

The method of any one of clauses 11 to 20, wherein the toluene per month is compared to a reactor rinsed by a different method. The amount of loss is reduced by greater than or equal to 45%.

The method of any one of aspects 11-21, wherein the amount of nitrogen consumed by the reactor is reduced by greater than or equal to 90% compared to a reactor flushed by a different method.

Concrete aspect 23: A system for controlling pressure in a pressure vessel, comprising: a pressure vessel comprising a vapor injection valve and a vapor release valve, wherein the pressure vessel is configured to receive a flow of irrigation fluid introduced into the pressure vessel When the pressure in the pressure vessel reaches a minimum, the first vapor stream is passed through the vapor injection valve and into the pressure vessel; and when the pressure in the pressure vessel reaches a maximum, the second vapor stream is passed The vapor releases the valve and exits the pressure vessel, wherein the minimum and the maximum are different.

In general, the invention may alternatively comprise, consist of, or consist essentially of any suitable components disclosed herein. The invention may additionally or alternatively be formulated so as to be free or substantially free of any components, materials, ingredients, adjuvants that are used in prior art compositions or otherwise are not necessary to achieve the function and/or purpose of the invention. Or species. All ranges of endpoints for the same component or property are included and can be independently combined (eg, "less than or equal to 25% by weight, or 5% to 20% by weight" ranges include "5 to 25% by weight" "The endpoint of the range and all intermediate values, etc.". The disclosure of a narrower range or a particular group other than a broader range is not a waiver of the broader scope or larger group. "Combination" includes blends, mixtures, alloys, reaction products, and the like. Furthermore, the terms "first", "second", etc. in this document do not mean any Order, quantity, or importance, but to indicate that one component is different from the other. The terms "a", "an", "the", "the" and "the" Or clearly contradictory to the context. “or” means “and/or”. The suffix "(s)" as used herein is intended to include both the singular and the plural of the terms which are modified to include one or more of the terms (eg, the film (s) includes one or more films). Throughout the specification, "a particular aspect", "another embodiment", "an embodiment", or the like, is meant to refer to the particular elements (such as features, structures, and / or features are included in at least one specific aspect described herein and may or may not be present in other specific aspects. In addition, it is to be understood that the described elements may be combined in various embodiments in any suitable manner.

The modifier "about" used in relation to a quantity includes the stated value and has the meaning specified by the context (eg, including the degree of error associated with a particular quantity of measurement). The designation "+10%" means that the measured value can be from the negative 10% of the stated value to the positive 10% amount. The terms "front", "back", "bottom", and/or "top, unless otherwise indicated, are used herein for convenience of description only and are not limited to any one location or spatial orientation. "arbitrary" or " "Optionally" means that the event or circumstance described thereafter may or may not occur, and that the description includes examples of the occurrence of the event and examples in which the event does not occur. Unless otherwise defined, the technical and scientific terms used herein have The same meaning as commonly understood by one of ordinary skill in the art is recognized. "Combination" includes blends, mixtures, alloys, reaction products, and the like.

Unless otherwise indicated, each of the foregoing groups may be unsubstituted or substituted, provided that the substitution does not significantly adversely affect the synthesis, stability, or use of the compound. The term "substituted" as used herein means that at least one hydrogen on a specified atom or group is replaced by another group, provided that the normal valence of the specified atom is not exceeded. When the substituent is a pendant oxy group (i.e., =0), the two hydrogens on the atom are replaced. Combinations of substituents and/or variables are permissible provided that the substitution does not significantly adversely affect the synthesis or use of the compound. Exemplary groups that may be present at the "substituted" position include, but are not limited to, cyano; hydroxy; nitro; azide; alkyl fluorenyl (eg, _C2-6 alkanoyl, eg, fluorenyl); Carboxamido; C _1-6 or C _1-3 alkyl, cycloalkyl, alkenyl, and alkynyl (which includes at least one unsaturated linkage and from 2 to 8, or 2 to 6 a group of a carbon atom; C _1-6 or C _1-3 alkoxy; C _6-10 aryloxy, such as phenoxy; C _1-6 alkylthio; C _1-6 or C _1-3 Alkylenesulfonyl; _C1-6 or _C1-3 alkanesulfonyl; an amine di( _C1-6 or _C1-3 )alkyl; a _C6-12 aryl having at least one aromatic ring ( For example, phenyl, biphenyl, naphthyl, or the like, each ring being a substituted or unsubstituted aromatic; having from 1 to 3 separate or fused rings and from 6 to 18 ring carbon atoms a C _7-19 arylalkyl group; or an aryl alkoxy group having 1 to 3 divided or fused rings and an arylalkoxy group having from 6 to 18 ring carbon atoms, exemplified by a benzyloxy group .

All cited patents, patent applications, and other references are herein incorporated by reference in their entirety. However, if a term in this application conflicts or conflicts with a term in the incorporated reference, the term from the present application takes precedence over the conflict from the incorporated reference. language.

Although specific specific aspects have been described, the applicant or other skilled artisan can produce alternatives, modifications, variations, improvements, and substantial equivalents that are presently unforeseen or may be unforeseen. Accordingly, the appended claims are intended to cover all such alternatives, modifications, modifications,

10‧‧‧ Pressure control method

12‧‧‧ fluid flushing flow

14‧‧‧ Pressure vessel

16‧‧‧First vapor stream

18‧‧‧Vapor injection valve

20‧‧‧Second vapor flow

22‧‧‧Vapor release valve

24‧‧‧ merged line

26‧‧‧ pump

28‧‧‧heater

30‧‧‧Flow controller

32‧‧‧Reactor

Claims (20)

A method of controlling pressure in a pressure vessel, comprising: introducing a flow of a flushing fluid into a pressure vessel, wherein the pressure vessel comprises a vapor injection valve and a vapor release valve; and when the pressure in the pressure vessel reaches a minimum, the first vapor is Flowing through the vapor injection valve and into the pressure vessel; and when the pressure in the pressure vessel reaches a maximum, passing a second vapor stream through the vapor release valve and exiting the pressure vessel, wherein the minimum and maximum The values are different. The method of claim 1, wherein the rinsing fluid stream comprises an aromatic solvent, an organic liquid having a boiling point of less than or equal to 300 ° C, or a combination comprising at least one of the foregoing, preferably wherein the rinsing fluid comprises toluene . The method of claim 1 or 2, wherein the first vapor stream comprises an inert gas, preferably wherein the first vapor stream comprises nitrogen, methane gas, ethane gas, or a combination comprising at least one of the foregoing. . The method of claim 1 or 2, wherein the second vapor stream comprises the flushing fluid in a gas phase. The method of claim 1 or 2, wherein the temperature in the pressure vessel is from 80 ° C to 250 ° C. The method of claim 1 or 2, wherein the pressure in the pressure vessel has a minimum value of 10 kPa to 500 kPa, and wherein the pressure in the pressure vessel has a maximum value of 50 kPa to 1000 kPa. . Such as the method of claim 1 or 2, wherein the pressure The minimum value of the pressure in the vessel differs from the maximum value of the pressure in the pressure vessel by greater than or equal to 10 kPa. The method of claim 1 or 2, wherein the flushing fluid flow is advanced by a pump, wherein the pump operates independently of the pressure in the pressure vessel. The method of claim 1 or 2, wherein the pressure vessel comprises steel, a composite material, a polymeric material, or a combination comprising at least one of the foregoing. A method of rinsing a reactor, comprising: introducing a flow of a flushing fluid into a pressure vessel, wherein the pressure vessel comprises a vapor injection valve and a vapor release valve; and when the pressure in the pressure vessel reaches a minimum, passing the first vapor stream Vapor is injected into the valve and into the pressure vessel; when the pressure in the pressure vessel reaches a maximum, a second vapor stream is passed through the vapor release valve and exits the pressure vessel, wherein the minimum value and the maximum value are different Extracting a portion of the flushing fluid stream from the pressure vessel; and flowing the portion of the flushing fluid through the reactor to flush the reactor. The method of claim 10, wherein the extracted portion of the flushing fluid is monitored by a flow controller before passing through the reactor. The method of claim 10, wherein the rinsing of the reactor is a closed loop system. The method of claim 10, wherein the rinsing fluid stream comprises an aromatic solvent and an organic liquid having a boiling point lower than or equal to 300 ° C. The body, or a combination comprising at least one of the foregoing, preferably wherein the rinse fluid comprises toluene. The method of claim 10, wherein the first vapor stream comprises an inert gas, preferably wherein the first vapor stream comprises nitrogen, methane gas, ethane gas, or a combination comprising at least one of the foregoing. . The method of claim 10, wherein the temperature in the pressure vessel is from 80 ° C to 250 ° C, wherein the pressure in the pressure vessel has a minimum value of 10 kPa to 500 kPa, and wherein the pressure vessel The maximum pressure in the range is 50 kPa to 1000 kPa. The method of claim 10, wherein the minimum value of the pressure in the pressure vessel differs from the maximum value of the pressure in the pressure vessel by greater than or equal to 10 kPa. The method of claim 10, wherein the flushing fluid flow is advanced by a pump, wherein the pump operates independently of the pressure in the pressure vessel. The method of claim 10 or 11, wherein the amount of toluene lost per month is reduced by greater than or equal to 45% compared to a reactor flushed by a different method. The method of claim 10, wherein the amount of nitrogen consumed by the reactor is reduced by greater than or equal to 90% compared to a reactor flushed by a different method. A system for controlling pressure in a pressure vessel, comprising: a pressure vessel comprising a vapor injection valve and a vapor release valve, wherein the pressure vessel is configured to: Receiving a flow of flushing fluid introduced into the pressure vessel; when the pressure in the pressure vessel reaches a minimum, passing a first vapor stream through the vapor injection valve and into the pressure vessel; and when the pressure in the pressure vessel When the maximum is reached, a second vapor stream is passed through the vapor release valve and exits the pressure vessel, wherein the minimum and the maximum are different.